Refrigeration



April 5, 1941. R. s. TAYLOR 2,238,138

REFRIGERATION Original Filed May 12, 1959 2 Sheets-Sheet 1 ATTORNEY.

Apr-i115, 1941. r R. s. TAYLOR REFRIGERATION 2 Sheets-Sheet 2 Original Filed May 12, 1939 wjazjyzljNTOR.

:ATTORNEY.

1113 Apr. 15, 1941 REFRIGERATION Robert S. Taylor, Evansville, Ind., assignor to Servel, Inc., New York, N. Y., a corporation of Delaware Original application May 12, 1939, Serial no.

273,195. Divided and this application April 24, 1940, Serial No. 331,290

3 Claims. 629 1195) absorption liquid formed in the absorber is divided into two streams. One of these streams is brought into heat exchange relation with hot weak absorption fluid flowing from the generator to the absorber, while the other stream is brought into contact with the vapor produced in the generator. The first stream serves to cool the weak absorption liquid to substantially absorber temperature, while at the same time being itself heated to substantially generator temperature.

The other stream serves to'cool the vapor produced in the generator to substantially condenser temperature, thus causing the condensation of vapor of absorption liquid from the mixture of this vapor with refrigerant vapor. At the same time, this other stream of strong absorption liquid is heated by the vapors to substantially generator temperature.

Further objects and advantages of my invention will be apparent from the following description considered in connection with the accompanying drawings which form part of this specification and of which:

Fig. l is a cross-sectional view showing one embodiment of my invention; and

Fig. 2 is a similar view showing another embodiment.

Referring more particularly to Fig. 1, reference character I 0 designates generally a generator consisting of an outer shell ll through which extends a flue l2. The flue is arranged to be heated in any suitable manner, as by the gas burner I3. A partition I4 divides the annular space between the shell II and flue l2 into a chamber I5 and a chamber IS. A vapor dome I1 is provided at the upper side of chamber I 5. A vapor lift pipe l8 extends to within chamber l5 and is formed with an open lower end and one or more apertures I9. The upper end of pipe l8 opens into a standpipe 20, the lower end of which communicates with the liquid chamber 16.

A conduit 2| leads from the upper end of pipe H erably at the lowermost edges of the plates so thatliquid may flow along the bottom of the analyzer, thus preventing stagnation of liquid between the plates. The apertures 26 are below the uppermost edges of the plates so that vapor in passing through them is forced to bubble through the liquid. A downwardly extending leg 21 communicates with the same end of the analyzer to which is connected conduit 2 l. A conduit 28 connects the lower end of leg 21 with chamber 15 of the generator.

The opposite end of the analyzer is provided with an upwardly extending leg 29, to the upper end of which is connected a conduit 30 which leads to a condenser 3|. As shown, the condenser is air cooled, heat radiating fins 32 being provided for the transfer of heat to the air. The lower end of the condenser is connected to a pipe 33 which leads to the upper part of an evaporator coil 34. This coil is disposed within the region to be refrigerated, which region is preferably enclosed by means of heat insulating walls 35.

The lower end 0 fthe evaporator is connected by means of a conduit 36 to a compartment 31 formed in a gas heat exchanger 33. The other end of this compartment is connected by a conduit 39 to the upper part of an absorber vessel 40.

The absorber is provided with a plurality of transverse horizontal plates 4| formed with apertures 42 which are surrounded by raised rims 43, the apertures in adjacent plates being out of alignment. A conduit 44 communicates with the absorber vessel below the lowermost plate 4| therein and extends within the compartment 3'! formed in gas heat exchanger 38 and communicates with a space Bl at the upper end of the heat exchanger. A conduit 62 connects chamber 6i with the upper end of the evaporator coil 34. A conduit 63 also communicates with chamber BI and with one end of a vessel 64 having substantial volume. Conduit 33 connects the other end of this vessel with the outlet of condenser 3l.

A coil for cooling fluid is in heat exchange relation with absorber 40. The upper end of this coil is connected by means of a conduit 46 with the upper end of a condenser 1, while the lower end of the condenser is connected to the lower end of coil 45 by means'of a conduit 48.

Coil 45, conduit 46, condenser 47, and conduit 48 form a closed system which is entirely out of communication with the refrigerating system proper. The lower end of absorber is formed as a liquid sump 49. A conduit connects this sump with that end of analyzer 22 which is provided with the upwardly extending leg 29. A conduit 5| connects sump 49 with the outer member 52 of a liquid heat exchanger 53. The opposite end of member 52 is connected by means of a conduit 54 with the downwardly extending leg 21 of the analyzer. A conduit communicates with the lower part of liquid chamber I6 of the generator and is connected to the inner member 56 of the liquid heat exchanger. A conduit 51 is connected to the other end of the inner member 56 and communicates with the upper part of an absorber 40 above the uppermost plate 4| therein. If desired, heat transfer fins 58 may be placed on conduit 51.

The above described device operates as follows:

The apparatus is charged with a refrigerant, such as ammonia, dissolved in a liquid absorbent such as water. Inert gas, such as hydrogen, is also introduced into the apparatus.

Upon application of heat to the generator 10, vapor is produced in both chambers l5 and Hi, this vapor consisting primarily of ammonia vapor, but unavoidably also including some water vapor. The vapor produced in chamber I5 accumulates in the dome I1 and depresses the liquid level until the port I9 is uncovered. Thereupon, vapor enters the pipe [8 through the port and, in well known manner, serves to lift liquid upwardly through the pipe l8 whence it is discharged into the pipe 20. The vapor produced in the chamber l6 passes upwardly through the pipe 20 and joins the vapor from the pipe I8.

The vapor which thus reaches the upper end of stand-pipe 20 passes through conduit 2| to the analyzer 22, where the vapor is brought into contact with strong and relatively cold absorption liquid. The temperature of the vapor is reduced and substantially all of the water vapor is condensed, it having a higher boiling point than the ammonia. The ammonia vapor is cooled by contact with the strong liquid, but not sufliciently to cause its condensation. Due to the fact that the liquid already contains a large amount of ammonia in solution, it is not able to absorb the ammonia vapor and the latter passes into the upwardly extending leg 29 practically freed from water vapor. At the same time, the strong absorption liquid has been heated by contact with the hot vapors and some of the ammonia has been driven from solution therein, and likewise passes into the upwardly extending leg 29. From here duit M, thus being brought into heat exchange relation with warmer gas in the space 31 and an exchange of heat takes place.

The mixture of inert gas and refrigerant vapor is introduced into the lower part of the absorber and passes upwardly through the apertures 42 formed in the plates 4 l. As will be presently explained, weak absorption liquid is introduced into the upper part of the absorber through the conduit 51 and forms pools on the plates. As soon as these pools have reached a sufficient depth, liquid overflows the rims 43. Thus, the gaseous mixture is forced to pass upwardly through absorption liquid cascading downwardly through the absorber, with the result that the refrigerant vapor is absorbed. The inert gas, on the other hand, not being absorbable to any great extent by the water, flows out from the top of the absorber through the conduit 39 to the space 31 in the gas heat exchanger.

The absorption process is accompanied by the generation of heat and consequently the inert gas is heated. As above explained, this heat is given up to the cold mixture of inert gas and refrigerant vapor passing through the condult 44. From the upper end of space 31 the inert gas passes through the conduit 36 to the lower end of the evaporator, through which it flows counter-current to the refrigerant.

The absorber is located at a lower levelthan the evaporator and the circulation of gas between and through these vessels is caused by virtue of the fact that the mixture of refrigerant vapor and inert gas present in conduit 44 has a greater specific gravity than the substantially pure inert gas present in the space 3! of the heat exchanger.

the ammonia vapor passes through conduit 3|] to condenser 3|, where it is cooled by giving up heat to the air in contact with fins 32. Due to this cooling, the ammonia vapor is condensed and the liquid ammonia flows from the condenser by gravity through conduit 33 to the evaporator 34.

Inert gas is introduced into the evaporator through conduit 35, as will be explained hereinafter, with the result that'the partial pressure of Coil 45 contains a fluid which, under the pressure existing in the coil, has a boiling point, substantially the same as the temperature which it is desired to maintain in the absorber. Consequently the heat resulting from the absorption process flows from the absorber to the fluid within coil 45, and causes such liquid to boil. The vapor produced flows through conduit 45 to the condenser 41, where its temperature is reduced and it is condensed. The condensate flows by gravity through the conduit 48 back to the lower end of the coil 45. i

The strong absorption liquid formed in the absorber 40 collects in the sump 49, whence it flows in two streams, one passing through the conduit 50, while the other passes through the conduit 5|. The liquid whichv flows through thme conduit 50 is introduced into the analyzer 22 where, in the manner previously described, it serves to cool the hot mixture of vapors coming from the generator, with the result that Water vapor present in this mixture is condensed. At the same time, the strong absorption liquidis heated by the vapors to substantially generator temperature. From the downwardly extending leg 21 this preheated strong absorption liquid flows through the conduit 28 to the generator chamber l5.

The strong absorption liquid which passes through the conduit 5| from the sump enters the outer member 52 of the liquid heat exchanger where it is brought into heat exchange relation with hot weak absorption liquid flowing from chamber I6 of the generator. This portion of the strong absorption liquid is preheated. to substantially generator temperature and flows through the conduit 59 to join the absorption liquid which has passed through the analyzer and flows together with it through the conduit 28.

The upper end of standpipe I8 is at a higher elevation than the top of the absorber 40. The liquid level is maintained in pipe 20 at such a height that liquid will flow by gravity from the chamber I6 through the conduit 55, the irmer member 56 of the heat exchanger 53 and the conduit 51 to the upper part of the absorber.

In flowing through the heat exchanger, this liquid gives up heat to the cooler strong absorption liquid in the outer member 52. It may further be cooled through radiation of heat from the fins 58. I

Under normal operating conditions vessel 64 contains chiefly hydrogen gas which is substantially stagnant therein. The pressure existing within the system is such that ammonia gas is condensed at the temperature in the condenser I flows upwardly through conduit 33 to the vessel 64, thus displacing hydrogen gas therefrom. The displaced gas flows through the conduit 63 to the space Si in the gas heat exchanger. The ammonia vapor introduced into vessel 64 remains there until the temperature of the cooling air is decreased, whereupon the lower pressure resulting in the condenser withdraws the ammonia vapor from the vessel. Thus, during periods of high air temperature, a certain amount of refrlgerant is withdrawn from active participation in the system. 7

In the embodiment illustrated in Fig. 2, parts which correspond to those in Fig. 1 are designated by the same reference characters. The at between the two embodiments resides chiefly in the fact that, in Fig. 2, two chambers ltd and l5b, separated by a partition Ila, are provided in the generator. A conduit 28a connects the analyzer 22 with chamber a, while a conduit 54a, connects the outer member 52 of the liquid heat exchanger 53 with chamber lib. Conduits 18a and l8b extend from within chambers Ma and lib, respectively, to the upper part of standpipe 20. Otherwise, the apparatus shown in this flgure'is essentially the same as that shown in Fig. 1.

Likewise, the operation of this apparatus is similar to that of the apparatus illustrated in Fig. 1, with the exception that the strong absorption liquid which flows from the absorber through the analyzer 22 is lifted to the upper part of the conduit independently of the strong absorption liquid which flows from the absorber through the heat exchanger 52. Due to the fact that separate vapor lift's are provided for these two streams, the division of the strong absorption liquid between the two may be determined by the lifting effects of the two vapor lifts.

The relative amounts of strong absorption liquid flowing through the analyzer 22 and the heat exchanger 53, respectively, should be so regulated as to be in proportion to the amount of heat which it is desired to take up from the vapor and the weak absorption liquid, respectively,

While I have illustrated and described two more or less specific embodiments of my invention, it is to be understood that this has been done for purposes of illustration only and the scope of my invention is not to be limited. thereby, but is to be determined by the following claims. e

What is claimed is: 1. In an absorption refrigerating apparatus, a generator including a plurality of vapor liquid lifts, an analyzer, an absorber, means for conducting weak absorption liquid from said generator to said absorber, means for conducting a portion of the strong absorption liquid from said absorber in heat exchange relation with said weak absorption liquid to one of said lifts, means for conducting another portion of said weak absorption liquid from said absorber to said analyzer, means for conducting liquid from said analyzer to another of said lifts, and means for conducting vapor from said generator to said analyzer.

2. That improvement in the art of refrigeration which includes absorbing refrigerant vapor in an absorption liquid to form a strong solution, flowing a portion of said strong solution to a region of high temperature to evaporate refrigerant vapor therefrom and to form a weak solution, passing said vapor in direct contact with another portion of said strong solution, transferring heat from said weak solution to the first mentioned portion of said strong solution, separately raising said portions to a higher elevation by the ap-' plication of heat thereto, and uniting said portions after they have been elevated.

3. That improvement in the art of refrigeration which includes absorbing refrigerant vapor in an. absorption liquid to form a strong solution, flowtion of heat thereto at rates proportional to the amount of heat to be taken from said weak solution and from said vapor, respectively, and uniting said portions after they have been elevated.

. nonnn'r s. TAYLOR. 

